WO2009023252A1 - Configurations et procédés d'amélioration de la récupération de liquides de gaz naturel - Google Patents

Configurations et procédés d'amélioration de la récupération de liquides de gaz naturel Download PDF

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Publication number
WO2009023252A1
WO2009023252A1 PCT/US2008/009736 US2008009736W WO2009023252A1 WO 2009023252 A1 WO2009023252 A1 WO 2009023252A1 US 2008009736 W US2008009736 W US 2008009736W WO 2009023252 A1 WO2009023252 A1 WO 2009023252A1
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WIPO (PCT)
Prior art keywords
column
feed gas
recovery
plant
product
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PCT/US2008/009736
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English (en)
Inventor
John Mak
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Fluor Technologies Corporation
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Publication date
Application filed by Fluor Technologies Corporation filed Critical Fluor Technologies Corporation
Priority to MX2010001472A priority Critical patent/MX336113B/es
Priority to US12/669,025 priority patent/US9103585B2/en
Priority to CN200880103754.2A priority patent/CN101815915B/zh
Priority to EA201070277A priority patent/EA017240B1/ru
Priority to AU2008287322A priority patent/AU2008287322B2/en
Priority to EP08795331A priority patent/EP2185878A1/fr
Priority to CA2694149A priority patent/CA2694149A1/fr
Publication of WO2009023252A1 publication Critical patent/WO2009023252A1/fr

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
    • C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/28—Propane and butane
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/88—Quasi-closed internal refrigeration or heat pump cycle, if not otherwise provided
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/02—Control in general, load changes, different modes ("runs"), measurements

Definitions

  • the field of the invention is configurations and methods of processing natural gas, especially as it relates to flexible recovery of natural gas liquids (NGL) from natural gas.
  • NNL natural gas liquids
  • a feed gas stream under pressure is cooled by a heat exchanger, typically using propane refrigeration when the feed gas is rich (containing more than 5% C3+ components) and as the gas cools, liquids condense from the cooled gas.
  • the liquids are then expanded and fractionated in a distillation column (e.g., de-deethanizer or demethanizer) to separate residual components such as methane, nitrogen and other volatile gases as overhead vapor from the desired C2, C3 and heavier components.
  • a distillation column e.g., de-deethanizer or demethanizer
  • Rambo et al. describe in U.S. Pat. No. 5,890,378 a system in which the absorber is refluxed, in which the deethanizer condenser provides the reflux for both the absorber and the deethanizer while the cooling requirements are met using a turbo expander and propane refrigeration.
  • the absorber and the deethanizer operate at substantially the same pressure.
  • Rambo's configuration advantageously reduces capital cost for equipment associated with providing reflux for the absorption section and the de-deethanizer, high ethane recovery of 80% becomes difficult when feed gas pressure is less than 1,000 psig due to lower turbo expansion cooling while reducing absorber pressure.
  • a turbo-expander is employed to provide cooling of the feed gas for high propane or ethane recovery.
  • Exemplary configurations are described, for example, in U.S. Pat. No. 4,278,457, and U.S. Pat. No. 4,854,955, to Campbell et al., in U.S. Pat. No. 5,953,935 to McDermott et al., in U.S. Pat. No. 6,244,070 to Elliott et al., or in U.S. Pat. No. 5,890,377 to Foglietta.
  • While such configurations may provide at least some advantages over other processes, they typically require modifications of turbo expanders and changes in operating conditions when the plants are changed from propane recovery mode to ethane recovery mode or vice versa, or when the feed gas composition changes over time.
  • These known configurations are typically designed to operate within a narrow range of feed gas compositions and inlet pressures with the use of propane refrigeration. In most cases, high recoveries are also limited by CO2 freezing in the demethanizer, and propane recovery will drop in most cases when operating on ethane rejection mode.
  • a twin reflux process described in U.S. Pat. No. 7,051,553 to Mak et al. has a configuration in which a first column receives two reflux streams: One reflux stream comprises a vapor portion of the NGL and the other reflux stream comprises a lean reflux provided by the overhead of the second distillation column. While such process is advantageous for varying ethane recovery levels to meet ethane market demand, it nevertheless requires external refrigeration and turbo expansion for feed gas cooling in order to maintain high recovery.
  • the present invention is directed to configurations and methods for NGL recovery from natural gas using a first column that can receive alternate reflux streams, and using a residue gas recycle stream to either form a lean and cold reflux stream or to provide refrigeration for a feed cooler.
  • the overhead product of a second column is then either used as first column feed or as reflux stream, hi such configurations and methods, it should be noted that the reflux stream is selected as a function of the desired NGL recovery.
  • a method of recovering NGL from natural gas includes a step of feeding a vapor portion of a cooled feed gas in a first column to thereby form a first column bottom product and a first column overhead product, and providing alternate first and second reflux streams to the first column, hi another step, the first column bottom product is fed to a second column to thereby produce a second column overhead and a second column bottom product, and in yet another step, the first column overhead product is compressed and a portion of the compressed first column overhead product is then expanded, hi still another step, expansion of the compressed first column overhead product is used to provide cooling to the feed gas when the second column overhead is used as the second reflux stream, and expansion of the compressed first column overhead product is used to provide cooling to the first column when the portion of the first column overhead product is used as the first reflux.
  • it is generally preferred that expansion of the second column overhead product is used to provide cooling to the first column.
  • the first column overhead product is compressed to pipeline pressure, and it is further preferred that the portion of the compressed first column overhead product is typically between 10% and 50% of the compressed first column overhead product.
  • the cooled feed gas is cooled using refrigeration content of the first column overhead product and/or a second column reboiler stream, and where desired, further cooling may be provided to the first column by expansion of the vapor portion. Alternatively, or additionally, further cooling may also be provided to the second column by expansion of a liquid portion of the cooled feed gas.
  • the second column is operated at a pressure that is higher than the operating pressure of the first column, typically at least 10-50 psi, and more typically 20-100 psi higher.
  • the second column bottom product comprises at least 99% of the propane contained in the feed gas and at least 80% of the ethane contained in the feed gas, and/or that ethane recovery in the second column bottom product is variable between 2% and 90% of the ethane contained in the feed gas. Therefore, contemplated second column bottom products will comprise at least 99% of the propane contained in the feed gas, while ethane recovery in the second column bottom product can be variable between 2% and 90% of the ethane contained in the feed gas.
  • a natural gas liquids recovery plant will typically comprise a first column that is fluidly coupled to a second column such that a first column bottom product is provided to the second column, wherein the first column is configured to allow refluxing using alternate first and second reflux streams.
  • Such plants will further include a compressor that is fluidly coupled to the first column and configured to compress a first column overhead, and further include a bypass conduit that is configured to provide a portion of compressed first column overhead to alternately a feed exchanger or the first column as the first reflux stream.
  • a second conduit is typically included and configured to provide a second column overhead to the first column as (a) a column feed when the portion of the compressed first column overhead is provided to the first column as the first reflux or (b) the second reflux stream when the portion of the compressed first column overhead is provided to the feed exchanger.
  • contemplated plants will further comprise one or more side reboilers that are thermally coupled to a feed gas conduit such as to allow cooling of the feed gas.
  • a separator is then fluidly coupled to the first column and configured such that the separator produces a vapor portion of a feed gas and a liquid portion of the feed gas.
  • an expansion device is coupled between the separator and the first column and configured to reduce pressure in the vapor portion and/or the liquid portion.
  • the bypass conduit includes one or more expansion devices (most typically a JT valve).
  • one or more compressors are configured to allow compression of the first column overhead to at least pipeline pressure.
  • plants will also include a second exchanger that further cools a feed gas using refrigeration content of the first column overhead.
  • the first column is configured to operate at a first pressure
  • the second column is configured to operate at a second pressure
  • the second pressure is higher than the first pressure.
  • the conduit is preferably configured to allow bypassing of between 10% and 50% of the entire compressed first column overhead product. Such bypass volume will typically allow variable recovery of between 2% and 90% of the ethane contained in the feed gas while maintaining a high recovery of propane (99% and higher).
  • Figure 1 is an exemplary configuration of an NGL recovery plant according to the inventive subject matter.
  • high NGL recovery e.g., at least 99% C3 and at least 90% C2
  • the plant is configured such that the first column can receive a reflux stream from one of two locations, wherein the reflux stream is selected as a function of the desired NGL recovery.
  • external refrigeration requirements are entirely eliminated in such configurations, and it should be further recognized that contemplated plants and methods will allow variable ethane recovery levels via switching valves that allow selection of one of the two reflux streams.
  • contemplated plants and methods employ a two-column NGL recovery configuration having an absorber and a distillation column, and a bypass through which a portion of the residue gas compressor discharge is recycled to thereby eliminate external refrigeration.
  • the absorber is configured to receive two alternate reflux streams, wherein one reflux stream is drawn from an overhead vapor from the column for C 3 recovery and wherein the other reflux stream is drawn from the residue gas for C 2 recovery.
  • Such plants allow C 2 recovery of at least 80% and C 3 recovery of at least 99% with the flexibility of varying C 2 recovery from 2% to 90% while maintaining 99% C 3 recovery.
  • Flexibility is achieved via a first column that receives a reflux stream from residual gas recycle during ethane recovery or a reflux stream from a second column during propane recovery or ethane rejection (in such case, residual gas recycle is used to supplement feed gas cooling via JT operation).
  • contemplated methods and configurations include a first and a second column utilizing high pressure residue gas recycle to eliminate external refrigeration.
  • the first column receives alternate reflux streams, wherein one reflux stream comprises the overhead vapor from the distillation column for C3 recovery, and wherein alternatively the reflux stream comprises a chilled residue recycle gas for C2 recovery.
  • Contemplated configurations are especially advantageous in application to NGL recovery that requires C2 recovery of at least 85% and C3 recovery of at least 99% and flexibility of varying C2 recovery from 2% to 90% while maintaining 99% C3 recovery. Therefore, high NGL recovery is achieved without external refrigeration by using residual gas recycle and a lean reflux stream.
  • an NGL recovery plant has a first column 58 that is fluidly coupled to a second column 59.
  • a natural gas feed 1 with a typical composition of 84% Cl, 7% C2, 5% C3, 3% CO2 (all numbers in mole percent) and the balance C4+ hydrocarbons enters the NGL plant at about 90 °F and about 1,000 psig and is split into two portions, stream 2 and stream 3.
  • stream 2 is cooled in side reboilers 52 and 53 of the second column, forming streams 4 and 5, with stream 5 being about -20 0 F.
  • Stream 3 is cooled in exchanger 51 using residual gas stream 8 forming stream 6 at about -28 °F to 40 °F.
  • the available heating duties from the side reboilers are significantly reduced and typically only the upper side reboiler 53 is utilized.
  • Streams 5 and 6 are combined to form stream 7 that is further cooled in heat exchanger 54 forming two phase stream 14 at about 5°F to -28°F.
  • the condensate is separated in the separator 56 forming liquids stream 22, while vapor stream 21 is expanded in expander 57 to stream 24 at about 450 psig and a temperature of about -60°F to about -90°F.
  • the power produced from the expander is preferably used to drive re-compressor 65.
  • Liquid stream 22 is letdown in pressure in JT valve 70 forming stream 15 at about 450 psig and about -30 0 F to about -50 °F and is fed to exchanger 54 for refrigerant recovery prior to fractionation in the second distillation column via stream 23. It should be noted that the above provided temperature ranges exemplarily demonstrate the operating conditions between ethane recovery and ethane rejection.
  • recycle flow can be significantly reduced or even eliminated.
  • Stream 11 is first chilled with residual gas in exchanger 51 forming stream 10 at about 30 0 F, then in exchanger 54 to about -30 °F forming stream 12, and for ethane recovery then in exchanger 55 forming stream 16 at about -110 °F.
  • JT valve 71 is closed and JT valve 90 is open and stream 16 is letdown in pressure in JT valve 90 to about 450 psig forming a lean reflux stream 25 at about -140 °F that is fed to the top tray of the first column.
  • JT valve 90 is closed, and the chilled recycle gas is letdown in pressure in JT valve 71 forming two phase stream 19 at about 450 psig, which is re-combined with the residual gas from exchanger 55 at about -50 °F, which provide chilling to the feed gas in exchanger 54 and 51 via stream 13.
  • the first column overhead vapor stream 18 is used as a refrigerant in chilling the feed gas and the recycle gas in heat exchangers 55, 54, and 51 prior to compression in residue gas re-compressor 65 and residual gas compressor 67.
  • the first column overhead vapor cools the recycle gas and that the second column overhead gas and the recycle gas is JT' d to so provide feed gas chilling during propane recovery.
  • operation may be switched to ethane recovery by refluxing the first column with the recycled residual gas.
  • switching between ethane recovery and propane recovery is achieved by changing valve positions: Valve 71 is closed and valve 90 is open during ethane recovery, and valve 71 is open and valve 90 is closed during propane recovery. Valve 73 is closed for propane recovery and open for ethane recovery, while valve 74 is closed for propane recovery and open for ethane recovery.
  • the first column 58 further produces bottoms stream 28, typically at about -100 0 F to about -115 0 F, which is pumped by pump 63 forming stream 32 at about 450 psig.
  • the column bottom stream acts as a refrigerant to provide reflux condensing duty in heat exchanger 60 of the second column, prior to feeding the second column as stream 33.
  • valve 91 is closed and valve 92 is open, resulting in partially condensation of the second column overhead stream 34 in condenser 60 to about -35 0 F, forming stream 35 that is separated in reflux drum 61 into a vapor stream 30 and liquid stream 37.
  • the liquid portion 37 is pumped by reflux pump 62 forming reflux stream 38 to the rectification section of the second column.
  • Second column 59 produces the NGL bottom product 39.
  • contemplated configurations may be used for ethane or propane recovery with repositioning valves.
  • the condenser 60 can be disabled, and the first column bottom liquid stream 32 is introduced directly to the top tray of the second column by closing valve 92 and opening valve 91, while the overhead vapor from the second column stream 31 (via 34, 35, and 30) is routed directly to the bottom of the first column by opening valve 74.
  • variable ethane recovery is desirable (e.g., from about 2% to about 90%)
  • the flow ratio between flow to the first column top tray and bottom tray of the first column can be varied: Increasing the flow of stream 31 relative to stream 29 via control valves 72 and 74 increases ethane recovery while reducing the relative flows correspondingly reduces ethane recovery.
  • stream 30 is used as reflux for the first column (for propane recovery)
  • the reflux is cooled by exchanger 55 against first column overhead product to form stream 26 that is further cooled by JT expansion to stream 27 in JT valve 73.
  • the second column overhead vapor is chilled and partially condensed using the refrigerant content of the first column bottoms producing a vapor and liquid stream.
  • the ethane rich vapor stream is further chilled by the first column overhead forming a reflux to the first column.
  • the second column overhead vapor is routed directly to the first column bottom for rectification and recovery of the ethane and heavier components.
  • Preferred NGL recovery operation includes switching valves that permit the changeover from propane recovery mode to ethane recovery mode or vice versa, wherein various ethane recovery levels can be achieved by splitting the second column overhead flow between the first column top tray and the first column bottom tray.
  • suitable feed gas streams it is contemplated that various feed gas streams are appropriate, and especially suitable fed gas streams may include various hydrocarbons of different molecular weight. With respect to the molecular weight of contemplated hydrocarbons, it is generally preferred that the feed gas stream predominantly includes C1-C6 hydrocarbons. However, suitable feed gas streams may additionally comprise acid gases (e.g., carbon dioxide, hydrogen sulfide) and other gaseous components (e.g., hydrogen). Consequently, particularly preferred feed gas streams are natural gas and natural gas liquids.
  • acid gases e.g., carbon dioxide, hydrogen sulfide
  • other gaseous components e.g., hydrogen
  • the cooling requirements for the first column are at least partially provided by product streams and recycle gas, and that the C2/C3 recovery can be varied by employing a different reflux stream.
  • the C2 recovery it is contemplated that such configurations provide at least 85%, more typically at least 88%, and most typically at least 90% recovery, while it is contemplated that C3 recovery will be at least 95%, more typically at least 98%, and most typically at least 99%. Further related configurations, contemplations, and methods are described in our International patent applications with the publication numbers WO 2005/045338 and WO 2007/014069, both of which are incorporated by reference herein.

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Abstract

Les centrales prévues pour la récupération de GNL à partir de gaz naturel emploient des courants de reflux alternés dans une première colonne et un courant de dérivation de gaz résiduaires, la dilatation des divers courants de traitement fournissant sensiblement toute la charge calorifique dans la centrale. Les centrales prévues ne présentent pas seulement une récupération flexible d'éthane comprise entre 2 % et 90 % tout en récupérant au moins 99 % de propane, mais elles réduisent également et éliminent plus habituellement la nécessité d'une réfrigération externe.
PCT/US2008/009736 2007-08-14 2008-08-13 Configurations et procédés d'amélioration de la récupération de liquides de gaz naturel WO2009023252A1 (fr)

Priority Applications (7)

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MX2010001472A MX336113B (es) 2007-08-14 2008-08-13 Configuraciones y metodos para recuperacion mejorada de liquidos de gas natural.
US12/669,025 US9103585B2 (en) 2007-08-14 2008-08-13 Configurations and methods for improved natural gas liquids recovery
CN200880103754.2A CN101815915B (zh) 2007-08-14 2008-08-13 用于改进的天然气液回收的配置和方法
EA201070277A EA017240B1 (ru) 2007-08-14 2008-08-13 Установка и способ для повышенного извлечения газоконденсатных жидкостей
AU2008287322A AU2008287322B2 (en) 2007-08-14 2008-08-13 Configurations and methods for improved natural gas liquids recovery
EP08795331A EP2185878A1 (fr) 2007-08-14 2008-08-13 Configurations et procédés d'amélioration de la récupération de liquides de gaz naturel
CA2694149A CA2694149A1 (fr) 2007-08-14 2008-08-13 Configurations et procedes d'amelioration de la recuperation de liquides de gaz naturel

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US95569707P 2007-08-14 2007-08-14
US60/955,697 2007-08-14

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CN (1) CN101815915B (fr)
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EA (1) EA017240B1 (fr)
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AU2008287322A1 (en) 2009-02-19
MX2010001472A (es) 2010-03-04
US20100206003A1 (en) 2010-08-19
CN101815915B (zh) 2014-04-09
US9103585B2 (en) 2015-08-11
MX336113B (es) 2016-01-08
EA017240B1 (ru) 2012-10-30
CN101815915A (zh) 2010-08-25
AU2008287322B2 (en) 2012-04-19
CA2694149A1 (fr) 2009-02-19
EA201070277A1 (ru) 2010-08-30
EP2185878A1 (fr) 2010-05-19

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